Propylene polymers incorporating polyethylene macromers

ABSTRACT

A polyolefin product is provided which comprises a branched olefin copolymer having an syndiotactic polypropylene backbone, polyethylene branches and, optionally, one or more comonomers. The total comonomer content of the branched olefin copolymer is from 0 to 20 mole percent. Also, the mass ratio of the syndiotactic polypropylene to the polyethylene ranges from 99.9:0.1 to 50:50. Additionally, a process is provided for preparing a branched olefin copolymer which comprises: 
     a) copolymerizing ethylene, optionally with one or more copolymerizable monomers, in a polymerization reaction under conditions sufficient to form copolymer having greater than 40% chain end-group unsaturation; 
     b) copolymerizing the product of a) with propylene and, optionally, one or more copolymerizable monomers, in a polymerization reactor under suitable polypropylene polymerization conditions using a chiral, stereorigid transition metal catalyst capable of producing syndiotactic polypropylene; and 
     c) recovering a branched olefin copolymer.

This application is a divisional of U.S. Ser. No. 09/020,307, filed Feb.6, 1998 (now U.S. Pat. No. 6,660,809, granted Dec. 9, 2003) which isbased on U.S. provisional applications 60/037,323, filed Feb. 7, 1997,No. 60/046,812, filed May 2, 1997, and No. 60/067,782, filed Dec. 10,1997.

FIELD OF THE INVENTION

The present invention relates to propylene polymers incorporatingmacromers and a method for the preparation of branched polypropyleneutilizing chiral, stereorigid transition metal catalyst compounds.

BACKGROUND OF THE INVENTION

Polypropylene and related polymers are known to have low melt strength.This is a significant deficiency in key application areas such asthermoforming, blow molding, and fiber spinning. Polyethylene on theother hand is used extensively in blown film applications requiring goodmelt strength. The limitations in the melt strength of polypropylenesshow up as excess sag in sheet extrusion, rapid thinning of walls inparts thermoformed in the melt phase, low draw-down ratios in extrusioncoating, poor bubble formation in extrusion foam materials, and relativeweakness in large-part blow molding. Thus, it would be highly desirableto produce polypropylene and related polymers having enhanced meltstrength as well as commercially valuable processability.

Increasing the melt strength of polymers such as polypropylene has beenan industrial goal for well over ten years, however, success has beenlimited. The desirable properties that have made low densitypolyethylene commercially successful are attributed in large part tohigh melt strength and excellent processability. Both of theseproperties are attributed to the presence of long chain branching whichis thought to occur under high pressure polymerization conditions.

There has been some success in increasing the melt strength ofpolypropylene. For example, EP 190 889 A2 discloses high energyirradiation of polypropylene to create what is believed to bepolypropylene having substantial free-end long branches of propyleneunits. EP 384 431 discloses the use of peroxide decomposition ofpolypropylene in the substantial absence of oxygen to obtain a similarproduct.

Other attempts to improve the melt properties of polypropylene includeU.S. Pat. No. 5,541,236, which introduces long chain branching bybridging two PP backbones to form H-type polymers, and U.S. Pat. No.5,514,761, which uses dienes incorporated in the backbones to achieve asimilar effect. However, it is difficult to avoid cross-linking and gelformation in such processes.

Thus, there is still a need for propylene polymers having improved meltstrength and good processability.

SUMMARY OF THE INVENTION

The present invention meets that need by providing a polyolefin productwhich comprises a branched olefin copolymer having an isotacticpolypropylene backbone, polyethylene branches and, optionally, one ormore comonomers. The total comonomer content of the branched olefincopolymer is from 0 to 20 mole percent. Also, the mass ratio of theisotactic polypropylene to the polyethylene ranges from 99.9:0.1 to50:50. Additionally, a process is provided for preparing a branchedolefin copolymer which comprises:

a) copolymerizing ethylene, optionally with one or more copolymerizablemonomers, in a polymerization reaction under conditions sufficient toform copolymer having greater than 40% chain end-group unsaturation;

b) copolymerizing the product of a) with propylene and, optionally, oneor more copolymerizable monomers, in a polymerization reactor undersuitable polypropylene polymerization conditions using a chiral,stereorigid transition metal catalyst capable of producing isotacticpolypropylene; and

c) recovering a branched olefin copolymer.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a graphic illustration of the GPC-FTIR data for the polymerproduced in Example 4.

FIG. 2 is a graphic illustration of the complex viscosity vs. shear ratecurve for the polymer products produced in Example 5 and ComparativeExample 7.

DETAILED DESCRIPTION OF THE INVENTION

The polyolefin compositions of this invention are comprised of branchedpolymers wherein the polymer backbone is derived from propylene and thepolymer branches are derived from polyethylene. The branches andbackbone are polymerized under coordination or insertion conditions withactivated transition metal organometallic catalyst compounds. Thebranches are composed of polyethylene which may exhibit crystalline,semi-crystalline or glassy properties suitable for hard phase domains inaccordance with the art understood meaning of those terms, and areattached to a polymeric backbone that may also be crystalline. Thebackbone is composed of stereospecific polypropylene and, optionally,one or more comonomers. In addition, the backbone has a melt point of80° C. or higher. Preferably, the backbone is isotactic polypropylene.These compositions are useful as thermoforming resins and exhibitimproved processability over current polypropylene compositions.

In the branched olefin copolymer of the present invention, the massratio of the isotactic polypropylene to the polyethylene ranges from99.9:0.1 to 50:50. Preferably, the mass ratio of the isotacticpolypropylene to the polyethylene ranges from 95:5 to 50:50.

As used herein, “isotactic polypropylene” is defined as having at least70% isotactic pentads according to analysis by ¹³C-NMR. “Highlyisotactic polypropylene” is defined as having at least 90% isotacticpentads according to analysis by ¹³C-NMR. “Syndiotactic polypropylene”is defined as polypropylene having at least 70% syndiotactic pentadsaccording to analysis by ¹³C-NMR. Preferably, the backbone of thepresent invention is highly isotactic polypropylene.

The Macromer Sidechains

The branches of the polymer (also referred to as “sidechains”) arecomprised of ethylene and, optionally, one or more comonomers.Preferably, the comonomers are chemical units capable of formingcrystalline or glassy polymeric segments under conditions of insertionpolymerization. Suitable comonomers include C₃-C₂₀ α-olefins, geminallydisubstituted monomers, C₅-C₂₅ cyclic olefins C₈-C₂₅ styrenic olefinsand lower carbon number (C₃-C₈) alkyl-substituted analogs of the cyclicand styrenic olefins. Thus, typically, the branches can comprise from85-100 mol % ethylene, and from 0-15 mol % comonomer, preferably 90-99mol % ethylene and 1-10 mol % comonomer, most preferably 94-98 mol %ethylene and 2-6 mol % comonomer. In particular, as the sidechain Mnincreases above about 3,000, it is preferable to introduce small amountsof comonomer to minimize embrittlement, e.g., about 0.2-4.0 mol. %comonomer. The selection of comonomer can be based upon properties otherthan crystallinity disrupting capability, for instance, a longer olefincomonomer, such as 1-octene, may be preferred over a shorter olefin suchas 1-butene for improved polyethylene film tear. For improvedpolyethylene film elasticity or barrier properties, a cyclic comonomersuch as norbornene or alkyl-substituted norbornene may be preferred overan α-olefin.

The sidechains can have narrow or broad molecular weight distribution(Mw/Mn), for example, from 1.1 to 30, typically 2-8. Additionally, thesidechains can have different comonomer compositions, e.g., includingthe orthogonal compositional distributions described in U.S. Pat. No.5,382,630 (CDBI>50%), incorporated by reference for purposes of U.S.patent practice. Optionally, mixtures of sidechains with differentmolecular weights and/or compositions may be used.

The M_(n) of the sidechains are within the range of from greater than orequal to 500 and less than or equal to 45,000. Preferably the M_(n) ofthe sidechains is from 1500 to 30,000, and more preferably the M_(n) isfrom 1500 to 25,000. A preferred branched olefinic copolymer within thisclass will have a melt enthalpy (ΔH_(m)) as measured by differentialscanning calorimetry of ≦90 cal/g (measured by integrating heat flowsrecorded at temperatures≧80° C. while scanning at ≧5° C./min).

Conditions sufficient to form the sidechain copolymer include usingsuitable ethylene and comonomer reactant ratios to assure the describedsidechain olefin-derived unit constitution, plus catalyst and processconditions conducive to forming the unsaturated chain ends. Theteachings of copending provisional application U.S. Ser. No. 60/037,323filed Feb. 7, 1997 are specific to suitable catalyst selection and useto prepare macromeric copolymer chains with a high yield of vinylunsaturation. Sidechains disclosed in U.S. S. No. 60/037,323 have vinylends and are olefin copolymer chains having a number average molecularweight (Mn) of about 1500 to 75,000, alternately 1500 to 25,154, thenumber average molecular weight being determined by gel permeationchromatography (GPC) at 145° C. Additionally, the ratio of vinyl groupsto total olefin group, in these side chains follows the formula: (vinylgroups/olefin groups)>(comonomer mole percentage+0.1)⁸×10⁸×b. a and btake the following sets of values: a=−0.24, b=0.8; a=−0.20, b=0.8;a=−0.18, b=0.83; a=−0.15, b=0.83; or a=−0.10, b=0.85. The total numberof vinyl groups per 1000 carbon atoms is greater than or equal to8000÷M_(n) in these macromers. And the number of vinyl groups isdetermined by ¹H-NMR at 125° C. M_(w)/M_(n) ranges from 2.083 to 5.666.The metallocene catalyst used in the step a) preparation of theunsaturation-containing macromer can be essentially any catalyst capableof insertion polymerization of ethylene, it can be one capable of highcomonomer incorporation capability (see below) or of low comonomerincorporation capability. Those of low incorporation capability aretypically those that are more congested at the metal coordination site,thus unbridged and substituted unbridged metallocene catalysts areparticularly suitable. See also the teachings of U.S. Pat. No. 5,498,809and international publications WO 94/19436 and WO 94/13715, describingmeans of preparing vinylidene-terminated ethylene-1-butene copolymers inhigh yields. See also, the teachings of copending application U.S. Ser.No. 08/651,030, filed May 21, 1996, as to the preparation ofethylene-isobutylene copolymers having high levels of vinylidenechain-end unsaturation. Throughout the description above, and below, thephrase “chain-end” or “terminal” when referring to unsaturation meansolefin unsaturation suitable for insertion polymerization whether or notlocated precisely at the terminus of a chain. All documents of thisparagraph are incorporated by reference for purposes of U.S. patentpractice.

In a particular embodiment polymeric unsaturation-containing macromerproduct suitable as branches for a subsequent copolymerization reactioncan be prepared under solution polymerization conditions with preferredmolar ratios of aluminum in the alkyl alumoxane activator, e.g., methylalumoxane (MAO), to transition metal. Preferably that level is greaterthan or equal to 20 and less than or equal to 175; more preferablygreater than or equal to 20 and less than or equal to 140; and, mostpreferably greater than or equal to 20 and less than or equal to 100.The temperature, pressure and time of reaction depend upon the selectedprocess but are generally within the normal ranges for a solutionprocess. Thus, temperatures can range from 20° C. to 200° C., preferablyfrom 30° C. to 150° C., more preferably from 50° C. to 140° C., and mostpreferably between 55° C. and 135° C. The pressures of the reactiongenerally can vary from atmospheric to 345 MPa, preferably to 182 MPa.For typical solution reactions, temperatures will typically range fromambient to 250° C. with pressures from ambient to 3.45 MPa. Thereactions can be run batchwise. Conditions for suitable slurry-typereactions are similar to solution conditions except reactiontemperatures are limited to those below the melt temperature of thepolymer. In an additional, alternative reaction configuration, asupercritical fluid medium can be used with temperatures up to 250° C.and pressures up to 345 MPa. Under high temperature and pressurereaction conditions, macromer product of lower molecular weight rangesare typically produced, e.g., M_(n), about 1,500.

Suitable catalyst compounds that when activated can achieve highchain-end unsaturations specifically include those identified above withrespect to the preparation of high vinyl or vinylidene-containingmacromers. Catalyst compounds which are suitable for preparing thebranched olefin copolymer of the present invention are discussed in moredetailed below.

The polypropylene macromers can have narrow or broad molecular weightdistribution (Mw/Mn), for example, from 1.5 to 5, typically 1.7 to 3.Optionally, mixtures of sidechains with different molecular weights maybe used.

Preferably, the macromers of the present invention are made usingsolution-phase conditions. Preferred solvents for solution phasereactions are selected on the basis of polymer solubility, volatilityand safety/health considerations. Non-polar alkanes or aromatics arepreferred.

The Polyolefin Backbone

The polyolefin backbone of the present invention is composed ofpropylene monomers and, optionally, one or more comonomers. In oneembodiment of the present invention, no comonomers are present in thepolyolefin backbone, resulting in a polymer having an isotacticpolypropylene backbone and polyethylene sidechains.

In another embodiment of the present invention, one or more comonomersare present in the backbone. Comonomers which are useful in the presentinvention include ethylene, C₄-C₂₀ α-olefins, and lower carbon number(C₃-C₈) alkyl substituted analogs of the cyclic and styrenic olefins.Other copolymerizable monomers include geminally disubstituted olefinssuch as isobutylene, C₅-C₂₅ cyclic olefins such as cyclopentene,norbornene and alkyl-substituted norbornenes, and styrenic monomers suchas styrene and alkyl substituted styrenes. Comonomers are selected foruse based on the desired properties of the polymer product and themetallocene employed will be selected for its ability to incorporate thedesired amount of olefins.

When comonomers are used, they preferably comprise from 3 to 20 molepercent of the branched olefin copolymer. More preferably, thecomonomers comprise from 5 to 17 mole percent of the branched olefincopolymer.

In another embodiment of the present invention, the backbone of thepresent invention contains syndiotactic polypropylene and, optionally,one or more comonomers. Essentially all of the backbone can besyndiotactic, resulting in a polymer having a syndiotactic polypropylenebackbone and polyethylene sidechains. Alternatively, the backbone can bea combination of syndiotactic and isotactic polypropylene with,optionally, one or more comonomers.

The mass of the backbone will typically comprise at least 40 wt % of thetotal polymer mass, that of the backbone and the sidechains together, sothe backbone typically will have a nominal weight-average molecularweight (M_(w)) weight of at least equal to or greater than about 60,000.The term nominal is used to indicate that direct measurement of M_(w) ofthe backbone is largely impossible but that characterization of thecopolymer product will exhibit measurements of M_(w) that correlate to aclose approximate weight of the polymeric backbone inclusive only of themonoolefin mer derivatives and the insertion moieties of thesidebranches when the macromer consists of less than 50% of the totalpolymer mass.

Catalysts

Catalysts which are useful for producing the branched polyolefin of thepresent invention include all catalysts which are capable of producingisotactic polypropylene and incorporating significant quantities of theisotactic polyethylene macromers of the present invention. Preferably,metallocene catalysts are used.

As used herein “metallocene” refers generally to compounds representedby the formula Cp_(m)MR_(n)X_(q) wherein Cp is a cyclopentadienyl ringwhich may be substituted, or derivative thereof which may besubstituted, M is a Group 4, 5, or 6 transition metal, for exampletitanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium,molybdenum and tungsten, R is a hydrocarbyl group or hydrocarboxy grouphaving from one to 20 carbon atoms, X is a halogen, and m=1-3, n=0-3,q=0-3, and the sum of m+n+q is equal to the oxidation state of thetransition metal.

Methods for making and using metallocenes are well known in the art. Forexample, metallocenes are detailed in U.S. Pat. Nos. 4,530,914;4,542,199; 4,769,910; 4,808,561; 4,871,705; 4,933,403; 4,937,299;5,017,714; 5,057,475; 5,120,867; 5,278,119; 5,304,614; 5,324,800;5,350,723; 5,391,790; and 5,635,573 each fully incorporated herein byreference.

Preferred metallocenes are those that are stereorigid and comprise aGroup 4, 5, or 6 transition metal, biscyclopentadienyl derivative,preferably bis-indenyl metallocene components having the followinggeneral structure:

wherein M¹ is a metal of Group 4, 5, or 6 of the Periodic Table, forexample titanium, zirconium, hafnium, vanadium, niobium, tantalum,chromium, molybdenum and tungsten, preferably, zirconium, hafnium andtitanium, most preferably zirconium and hafnium;

R¹ and R² are identical or different, are one of a hydrogen atom, aC₁-C₁₀ alkyl group, preferably a C₁-C₃ alkyl group, a C₁-C₁₀ alkoxygroup, preferably a C₁-C₃ alkoxy group, a C₆-C₁₀ aryl group, preferablya C₆-C₈ aryl group, a C₆-C₁₀ aryloxy group, preferably a C₆-C₈ aryloxygroup, a C₂-C₁₀ alkenyl group, preferably a C₂-C₄ alkenyl group, aC₇-C₄₀ arylalkyl group, preferably a C₇-C₁₀ arylalkyl group, a C₇-C₄₀alkylaryl group, preferably a C₇-C₁₂ alkylaryl group, a C₈-C₄₀arylalkenyl group, preferably a C₈-C₁₂ arylalkenyl group, or a halogenatom, preferably chlorine;

R³ and R⁴ are hydrogen atoms;

R⁵ and R⁶ are identical or different, preferably identical, are one of ahydrogen atom, halogen atom, preferably a fluorine, chlorine or bromineatom, a C₁-C₁₀ alkyl group, preferably a C₁-C₄ alkyl group, which may behalogenated, a C₆-C₁₀ aryl group, which may be halogenated, preferably aC₆-Cg aryl group, a C₂-C₁₀ alkenyl group, preferably a C₂-C₄ alkenylgroup, a C₇-C₄₀-arylalkyl group, preferably a C₇-C₁₀ arylalkyl group, aC₇-C₄₀ alkylaryl group, preferably a C₇-C₁₂ alkylaryl group, a C₈-C₄₀arylalkenyl group, preferably a C₈-C₁₂ arylalkenyl group, a —NR₂ ¹⁵,—SR¹⁵, —OR¹⁵, —OSiR₃ ¹⁵ or —PR₂ ¹⁵ radical, wherein R¹⁵ is one of ahalogen atom, preferably a chlorine atom, a C₁-C₁₀ alkyl group,preferably a C₁-C₃ alkyl group, or a C₆-C₁₀ aryl group, preferably aC₆-C₉ aryl group;

R⁷ is

 wherein:

R¹¹, R¹² and R¹³ are identical or different and are a hydrogen atom, ahalogen atom, a C₁-C₂₀ alkyl group, preferably a C₁-C₁₀ alkyl group, aC₁-C₂₀ fluoroalkyl group, preferably a C₁-C₁₀ fluoroalkyl group, aC₆-C₃₀ aryl group, preferably a C₆-C₂₀ aryl group, a C₆-C₃₀ fluoroarylgroup, preferably a C₆-C₂₀ fluoroaryl group, a C₁-C₂₀ alkoxy group,preferably a C₁-C₁₀ alkoxy group, a C₂-C₂₀ alkenyl group, preferably aC₂-C₁₀ alkenyl group, a C₇-C₄₀ arylalkyl group, preferably a C₇-C₂₀arylalkyl group, a C₈-C₄₀ arylalkenyl group, preferably a C₈-C₂₂arylalkenyl group, a C₇-C₄₀ alkylaryl group, preferably a C₇-C₂₀alkylaryl group or R¹¹ and R¹², or R¹¹ and R¹³, together with the atomsbinding them, can form ring systems;

M² is silicon, germanium or tin, preferably silicon or germanium, mostpreferably silicon;

R⁸ and R⁹ are identical or different and have the meanings stated forR¹¹;

m and n are identical or different and are zero, 1 or 2, preferably zeroor 1, m plus n being zero, 1 or 2, preferably zero or 1; and

the radicals R¹⁰ are identical or different and have the meanings statedfor R¹¹, R¹² and R¹³. Two adjacent R¹⁰ radicals can be joined togetherto form a ring system, preferably a ring system containing from about4-6 carbon atoms.

Alkyl refers to straight or branched chain substituents. Halogen(halogenated) is fluorine, chlorine, bromine or iodine atoms, preferablyfluorine or chlorine.

Particularly preferred metallocenes are compounds of the structures:

wherein:

M¹ is Zr or Hf, R¹ and R² are methyl or chlorine, and R⁵, R⁶ R⁸, R⁹,R¹⁰, R¹¹ and R¹² have the above-mentioned meanings.

The chiral metallocenes may be used as a racemate for the preparation ofhighly isotactic polypropylene polymers and copolymers. It is alsopossible to use the pure R or S form. An optically active polymer can beprepared with these pure stereoisomeric forms. Preferably the meso formof the metallocene is removed to ensure the center (i.e., the metalatom) provides stereoregular polymerization.

Separation of the stereoisomers can be accomplished by known literaturetechniques. For special products it is also possible to use rac/mesomixtures.

Generally, the metallocenes are prepared by a multi-step processinvolving repeated deprotonations/metallations of the aromatic ligandsand introduction of the bridge and the central atom by their halogenderivatives. The following reaction scheme illustrates this genericapproach:

Additional methods for preparing metallocenes of the present inventionare fully described in the Journal of Organometallic Chem., volume 288,(1958), pages 63-67, and in EP-A-320762, for preparation of themetallocenes described, both of which are herein fully incorporated byreference.

Illustrative but non-limiting examples of some preferred metallocenesinclude: Dimethylsilandiylbis (2-methyl-4-phenyl-1-indenyl)ZrCl₂Dimethylsilandiylbis(2-methyl-4,5-benzoindenyl)ZrCl₂;Dimethylsilandiylbis(2-methyl-4,6-diisopropylindenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-phenyl-1-indenyl)ZrCl₂;Dimethylsilandiylbis (2-ethyl-4-naphthyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(2-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4,6-trimethyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-t-butyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-4-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4-dimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(methylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(tetramethylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis (2-methyl-a-acenaphth-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2,4,7-trimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-1-indenyl)ZrCl₂,Phenyl(ethyl)silandiylbis(2-methyl-1-indenyl)ZrCl₂,Diphenylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-t-butyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,5,6-trimethyl-1-indenyl)ZrCl₂, and the like.

Some preferred metallocene catalyst components are described in detailin U.S. Pat. Nos. 5,149,819, 5,243,001, 5,239,022, 5,296,434 and5,276,208 all of which are herein fully incorporated by reference. Inaddition, the bis-amido and bis-arylamido transition metal catalysts ofU.S. Pat. No. 5,318,935 and copending U.S. patent application Ser. No.08/803,687, filed Feb. 24, 1997, and the α-diimine nickel catalystcomplexes of WO 96/23010 can be useful in incorporating the macromers ofthe present invention into the backbone.

Most preferably, the catalyst used to produce the branched polyolefin ofthe present invention is a dimethylsilyl-bridged bis-indenyl zirconoceneor hafnocene such as dimethylsilyl bis(2-methyl-indenyl) ZrCl₂,dimethylsilyl bis(2-methyl-4-phenyl-1-indenyl) ZrCl₂, dimethylsilylbis(2-methyl-4-(1-naphthyl)-1-indenyl) ZrCl₂, or dimethylsilylbis(indenyl)hafnium dimethyl.

Preferably, the catalysts used to produce the syndiotactic polypropylenebackbone of the present invention are those disclosed in U.S. Pat. Nos.4,892,851, 5,155,080, and 5,132,381, the disclosures of which are herebyincorporated by reference.

The terms “cocatalyst” and “activator” are used herein interchangeablyand are defined to be any compound or component which can activate abulky ligand transition metal compound or a metallocene, as definedabove. Alumoxane may be used as an activator. There are a variety ofmethods for preparing alumoxane, non-limiting examples of which aredescribed in U.S. Pat. Nos. 4,665,208, 4,952,540, 5,091,352, 5,206,199,5,204,419, 4,874,734, 4,924,018, 4,908,463, 4,968,827, 5,308,815,5,329,032, 5,248,801, 5,235,081, 5,157,137, 5,103,031 and EP-A-0 561476, EP-B1-0 279 586, EP-A-0 594-218 and WO 94/10180, each of which isfully incorporated herein by reference. It may be preferable to use avisually clear methylalumoxane. A cloudy or gelled alumoxane can befiltered to produce a clear solution or clear alumoxane can be decantedfrom the cloudy solution.

It is also within the scope of this invention to use ionizingactivators, neutral or ionic, or compounds such as tri(n-butyl)ammoniumtetrakis(pentaflurophenyl)boron, which ionize the neutral metallocenecompound. Such ionizing compounds may contain an active proton, or someother cation associated with but not coordinated or only looselycoordinated to the remaining ion of the ionizing compound. Combinationsof activators are also contemplated by the invention, for example,alumoxane and ionizing activators in combinations, see for example, WO94/07928.

Descriptions of ionic catalysts for coordination polymerizationcomprised of metallocene cations activated by non-coordinating anionsappear in the early work in EP-A-0 277 003, EP-A-0 277 004 and U.S. Pat.No. 5,198,401 and WO-A-92/00333 (incorporated herein by reference).These teach a preferred method of preparation wherein metallocenes (bisCp and monoCp) are protonated by an anion precursor such that analkyl/hydride group is abstracted from a transition metal to make itboth cationic and charge-balanced by the non-coordinating anion.

The term “noncoordinating anion” means an anion which either does notcoordinate to said cation or which is only weakly coordinated to saidcation thereby remaining sufficiently labile to be displaced by aneutral Lewis base. “Compatible” noncoordinating anions are those whichare not degraded to neutrality when the initially formed complexdecomposes. Further, the anion will not transfer an anionic substituentor fragment to the cation so as to cause it to form a neutral fourcoordinate metallocene compound and a neutral by-product from the anion.Noncoordinating anions useful in accordance with this invention arethose which are compatible, stabilize the metallocene cation in thesense of balancing its ionic charge in a+1 state, yet retain sufficientlability to permit displacement by an ethylenically or acetylenicallyunsaturated monomer during polymerization.

The use of ionizing ionic compounds not containing an active proton butcapable of producing the both the active metallocene cation and annoncoordinating anion is also known. See, EP-A-0 426 637 and EP-A-0 573403 (incorporated herein by reference). An additional method of makingthe ionic catalysts uses ionizing anion pre-cursors which are initiallyneutral Lewis acids but form the cation and anion upon ionizing reactionwith the metallocene compounds, for example the use oftris(pentafluorophenyl) boron. See EP-A-0 520 732 (incorporated hereinby reference). Ionic catalysts for addition polymerization can also beprepared by oxidation of the metal centers of transition metal compoundsby anion pre-cursors containing metallic oxidizing groups along with theanion groups, see EP-A-0 495 375 (incorporated herein by reference).

Where the metal ligands include halogen moieties (for example,bis-cyclopentadienyl zirconium dichloride) which are not capable ofionizing abstraction under standard conditions, they can be convertedvia known alkylation reactions with organometallic compounds such aslithium or aluminum hydrides or alkyls, alkylalumoxanes, Grignardreagents, etc. See EP-A-0 500 944 and EP-A1-0 570 982 (incorporatedherein by reference) for in situ processes describing the reaction ofalkyl aluminum compounds with dihalo-substituted metallocene compoundsprior to or with the addition of activating anionic compounds.

Support Materials

The metallocenes described herein are preferably supported using aporous particulate material, such as for example, talc, inorganicoxides, inorganic chlorides and resinous materials such as polyolefin orpolymeric compounds.

The most preferred support materials are porous inorganic oxidematerials, which include those from the Periodic Table of Elements ofGroups 2, 3, 4, 5, 13 or 14 metal oxides. Silica, alumina,silica-alumina, and mixtures thereof are particularly preferred. Otherinorganic oxides that may be employed either alone or in combinationwith the silica, alumina or silica-alumina are magnesia, titania,zirconia, and the like.

Preferably the support material is porous silica which has a surfacearea in the range of from about 10 to about 700 m²/g, a total porevolume in the range of from about 0.1 to about 4.0 cc/g and an averageparticle size in the range of from about 10 to about 500 μm. Morepreferably, the surface area is in the range of from about 50 to about500 m²/g, the pore volume is in the range of from about 0.5 to about 3.5cc/g and the average particle size is in the range of from about 20 toabout 200 μm. Most preferably the surface area is in the range of fromabout 100 to about 400 m²/g, the pore volume is in the range of fromabout 0.8 to about 3.0 cc/g and the average particle size is in therange of from about 30 to about 100 μm. The average pore size of typicalporous support materials is in the range of from about 10 to about 1000Å. Preferably, a support material is used that has an average porediameter of from about 50 to about 500 Å, and most preferably from about75 to about 350 Å. It may be particularly desirable to dehydrate thesilica at a temperature of from about 100° C. to about 800° C. anywherefrom about 3 to about 24 hours.

The metallocenes, activator and support material may be combined in anynumber of ways. Suitable support techniques are described in U.S. Pat.Nos. 4,808,561 and 4,701,432 (each fully incorporated herein byreference). Preferably the metallocenes and activator are combined andtheir reaction product supported on the porous support material asdescribed in U.S. Pat. No. 5,240,894 and WO 94/28034, WO 96/00243, andWO 96/00245 (each fully incorporated herein by reference.)Alternatively, the metallocenes may be preactivated separately and thencombined with the support material either separately or together. If themetallocenes are separately supported, then preferably, they are driedthen combined as a powder before use in polymerization.

Regardless of whether the metallocene and activator are separatelyprecontacted or whether the metallocene and activator are combined atonce, the total volume of reaction solution applied to porous support ispreferably less than about 4 times the total pore volume of the poroussupport, more preferably less than about 3 times the total pore volumeof the porous support and even more preferably in the range of from morethan about 1 to less than about 2.5 times the total pore volume of theporous support. Procedures for measuring the total pore volume of poroussupport are well known in the art. The preferred method is described inVolume 1, Experimental Methods in Catalyst Research, Academic Press,1968, pages 67-96.

Methods of supporting ionic catalysts comprising metallocene cations andnoncoordinating anions are described in WO 91/09882, WO 94/03506, WO96/04319 and U.S. Pat. No. 5,643,847 (incorporated herein by reference).The methods generally comprise either physical adsorption on traditionalpolymeric or inorganic supports that have been largely dehydrated anddehydroxylated, or using neutral anion precursors that are sufficientlystrong Lewis acids to activate retained hydroxy groups in silicacontaining inorganic oxide supports such that the Lewis acid becomescovalently bound and the hydrogen of the hydroxy group is available toprotonate the metallocene compounds.

The supported catalyst system may be used directly in polymerization orthe catalyst system may be prepolymerized using methods well known inthe art. For details regarding prepolymerization, see U.S. Pat. Nos.4,923,833 and 4,921,825, EP 0 279 863 and EP 0 354 893 each of which isfully incorporated herein by reference.

Polymerization Processes

The branched polyolefin of the present invention may be produced usingthe catalysts described above in any process including gas, slurry orsolution phase or high pressure autoclave processes. (As used herein,unless differentiated, “polymerization” includes copolymerization and“monomer” includes comonomer.) Additionally, combinations of the abovereactor types in multiple, series reactors and/or multiple reactionconditions and/or multiple catalyst configurations are explicitlyintended. Preferably, a gas or slurry phase process is used, mostpreferably a bulk liquid propylene polymerization process is used.

In the preferred embodiment, this invention is directed toward the bulkliquid polymerization and copolymerization of propylene in a slurry orgas phase polymerization process, particularly a slurry polymerizationprocess. Another embodiment involves copolymerization reactions ofpropylene with one or more comonomers. Such comonomers includealpha-olefin monomers having from 4 to 20 carbon atoms, preferably 4-12carbon atoms, for example alpha-olefin comonomers of ethylene, butene-1,pentene-1,4-methylpentene-1, hexene-1, octene-1, decene-1. Othersuitable comonomers include geminally disubstituted monomers, C₅-C₂₅cyclic olefins such as cyclopentene or norbornene, styrenic olefins suchas styrene, and lower carbon number (C₃-C₈) alkyl substituted analogs ofthe cyclic and styrenic olefins. In addition, comonomers such as polarvinyl, diolefins such as dienes, for example, 1,3-butadiene,1,4-hexadiene, norbornadiene or vinylnorbornene, acetylene and aldehydemonomers are suitable.

Typically in a gas phase polymerization process a continuous cycle isemployed wherein one part of the cycle of a reactor, a cycling gasstream, otherwise known as a recycle stream or fluidizing medium, isheated in the reactor by the heat of polymerization. The recycle streamusually contains one or more monomers continuously cycled through afluidized bed in the presence of a catalyst under reactive conditions.This heat is removed in another part of the cycle by a cooling systemexternal to the reactor. The recycle stream is withdrawn from thefluidized bed and recycled back into the reactor. Simultaneously,polymer product is withdrawn from the reactor and new or fresh monomeris added to replace the polymerized monomer. (See for example U.S. Pat.Nos. 4,543,399; 4,588,790; 5,028,670; 5,352,749; 5,405,922, and5,436,304 all of which are fully incorporated herein by reference.)

A slurry polymerization process generally uses pressures in the range offrom about 1 to about 500 atmospheres or even greater and temperaturesin the range of from −60° C. to about 280° C. In a slurrypolymerization, a suspension of solid, particulate polymer is formed ina liquid or supercritical polymerization medium to which propylene andcomonomers and often hydrogen along with catalyst are added. The liquidemployed in the polymerization medium can be, for example, an alkane ora cycloalkane. The medium employed should be liquid under the conditionsof polymerization and relatively inert such as hexane and isobutane. Inthe preferred embodiment, propylene serves as the polymerization diluentand the polymerization is carried out using a pressure of from about 200kPa to about 7,000 kPa at a temperature in the range of from about 50°C. to about 120° C.

The periods of time for each stage will depend upon the catalyst system,comonomer and reaction conditions. In general, propylene should behomopolymerized for a time period sufficient to yield a compositionhaving from about 10 to about 90 weight percent homopolymer based on thetotal weight of the polymer, preferably from about 20 to about 80 weightpercent, even more preferably from about 30 to about 70 homopolymerweight percent based on the total weight of the polymer.

The above-described temperatures, reaction times and other conditionsare considered suitable polypropylene polymerization conditions for thepurposes of this invention.

The polymerization may be conducted in batch or continuous mode and theentire polymerization may take place in one reactor or, preferably, thepolymerization may be carried out in a series of reactors. If reactorsin series are used, then the comonomer may be added to any reactor inthe series, however, preferably, the comonomer is added to the second orsubsequent reactor.

Hydrogen may be added to the polymerization system as a molecular weightregulator in the first and/or subsequent reactors depending upon theparticular properties of the product desired and the specificmetallocenes used. When metallocenes having different hydrogen responsesare used, the addition of hydrogen will affect the molecular weightdistribution of the polymer product accordingly. A preferred productform is to have the comonomer be present in the high molecular weightspecies of the total polymer composition to provide a favorable balanceof good film stretchability without breaking, coupled with lowextractables, low haze and good moisture barrier in the film.Accordingly in this preferred case, the same or lower levels of hydrogenare utilized during copolymerization as were used during polymerizationin the second or subsequent reactor.

For both polyethylene macromer product and branched polyolefinpreparation, it is known that many methods and permutations of theordering of addition of macromer and monomer species to the reactor arepossible, some more advantageous than others. For example, it is widelyknown in the art that preactivation of the metallocene with alumoxanebefore addition to a continuous solution-phase reactor yields higheractivities than continuous addition of metallocene and activator in twoseparate streams. Furthermore, it may be advantageous to controlprecontacting time to maximize catalyst effectiveness, e.g., avoidingexcessive aging of the activated catalyst composition.

It is preferable to use the polyethylene macromers such that they arepromptly functionalized or copolymerized after being prepared. Thehighly reactive vinyl groups appear to be susceptible to by-productreactions with adventitious impurities and, even, dimerization oraddition reactions with other unsaturated group-containing polymericchains. Thus maintaining in a cooled, inert environment afterpreparation and prompt subsequent use will optimize the effectiveness ofthe use of the polyethylene macromer product. A continuous processutilizing series reactors, or parallel reactors will thus be effective,the polyethylene macromer product being prepared in one and continuouslyintroduced into the other.

INDUSTRIAL UTILITY

The branched polyolefin polymers of the present invention exhibitimproved melt strength and shear thinning characteristics to standardpropylene copolymers. This results in improved processability of thepolymers, e.g. increased shear thinning and high output for a constantenergy input. These characteristics will result in improved processingin blow molding and thermoforming operations. For example, inthermoforming operations sag will be decreased and power consumptionwill be lowered in the extruders.

In an other embodiment the branched olefin copolymer has dual meltingpoints characteristic of crystalline polypropylene and crystallinepolyethylene.

In order that the invention may be more readily understood, reference ismade to the following examples, which are intended to illustrate theinvention but not to limit the scope thereof.

EXAMPLES

General

All polymerizations were performed in a 2-liter Zipperclave reactorequipped with a water jacket for temperature control. Liquids weremeasured into the reactor using calibrated sight glasses. High purity(>99.5%) toluene was purified by passing first through basic aluminaactivated at high temperature in nitrogen, followed by molecular sieveactivated at high temperature in nitrogen. Polymerization grade ethylenewas supplied directly in a nitrogen-jacketed line and used withoutfurther purification. Propylene was purified by passing throughactivated basic alumina and molecular sieves. Methylalumoxane (MAO, 10%in toluene) was received from Albemarle Inc. in stainless steelcylinders, divided into 1-liter glass containers, and stored in alaboratory glove-box at ambient temperature.

For the polymer synthesis, propylene was measured into the reactorthrough a calibrated container. To ensure the reaction medium waswell-mixed, a flat-paddle stirrer rotating at 750 rpm was used.

Reactor Preparation

The reactor was first cleaned by heating to 150° C. in toluene todissolve any polymer residues, then cooled and drained. Next, thereactor was heated using jacket water at 110° C. and the reactor waspurged with flowing nitrogen for a period of 30 minutes. Beforereaction, the reactor was further purged using 3 nitrogenpressurize/vent cycles (to 100 psi). The cycling served two purposes:(1) to thoroughly penetrate all dead ends such as pressure gauges topurge fugitive contaminants and (2) to pressure test the reactor.

Catalysts

All catalyst preparations were performed in an inert atmosphere with<1.5 ppm H₂O content. The catalyst system used in the synthesis ofmacromer was Cp₂ZrCl₂ activated with MAO. The catalyst systems used inthe synthesis of branched olefin copolymer were dimethylsilylbis(indenyl)hafnium dimethyl and dimethylsilyl bis(2-methyl indenyl)zirconium dichloride. The dimethylsilyl bis(indenyl)hafnium dimethyl wasactivated with [DMAH]⁺[(C₆F₅)₄B]⁺. The dimethylsilyl bis(2-methylindenyl) zirconium dichloride was activated with MAO. To maximizesolubility of the metallocene, toluene was used as a solvent. Thecatalyst was added to a stainless steel tube by pipette and transferredto the reactor.

Macromer Synthesis—General:

Ethylene was added to the reactor as needed to maintain total systempressure at the reported levels (semi-batch operation). Ethylene flowrate was monitored using a Matheson mass flow meter (model number8272-0424). To ensure the reaction medium was well-mixed, a flat-paddlestirrer rotating at 750 rpm was used.

Example 1

The reactor was simultaneously purged of nitrogen and pressure testedusing two ethylene fill/purge cycles (to 300 psig). Then, the reactorpressure was raised to ˜40 psi to maintain positive reactor pressureduring setup operations. Jacket water temperature was set to 120° C. and1200 milliliters of toluene were added to the reactor. The stirrer wasset to 750 rpm. Additional ethylene was added to maintain a positivereactor gauge pressure as gas phase ethylene was absorbed into solution.The system was allowed to reach a steady temperature. The ethylenepressure regulator was next set to 40 psig and ethylene was added to thesystem until a steady state was achieved as measured by zero ethyleneuptake. The reactor was isolated and a pulse of toluene pressurized to300 psig was used to force the catalyst solution from the addition tubeinto the reactor. The ethylene supply manifold was immediately opened tothe reactor in order to maintain a constant reactor pressure as ethylenewas consumed by reaction.

After 60 minutes of reaction, the reactor was isolated, cooled to roomtemperature and methanol was added to precipitate the macromer product.The yield was 48 g. The polymer product had an Mn of 7,500 and a vinylend group percentage of 73.

Example 2

The reactor was simultaneously purged of nitrogen and pressure testedusing two ethylene fill/purge cycles (to 300 psig). Then, the reactorpressure was raised to ˜40 psi to maintain positive reactor pressureduring setup operations. Jacket water temperature was set to 120° C. and1200 milliliters of toluene were added to the reactor. The stirrer wasset to 750 rpm. Additional ethylene was added to maintain a positivereactor gauge pressure as gas phase ethylene was absorbed into solution.The system was allowed to reach a steady temperature. The ethylenepressure regulator was next set to 40 psig and ethylene was added to thesystem until a steady state was achieved as measured by zero ethyleneuptake. The reactor was isolated and a pulse of toluene pressurized to300 psig was used to force the catalyst solution from the addition tubeinto the reactor. The ethylene supply manifold was immediately opened tothe reactor in order to maintain a constant reactor pressure as ethylenewas consumed by reaction.

After 20 minutes of reaction, the reactor was isolated, cooled to roomtemperature and methanol was added to precipitate the macromer product.The yield was 23.3 g. The polymer product had an Mn of 4,300 and a vinylend group percentage of 73.

Example 3

A 2-liter reactor was charged with toluene (1 L), propylene (150 mL), 10g of the polyethylene macromer from Example 1 and Triisobutylaluminum(2.0 mL of 1M solution in toluene). The reactor was heated to 90° C. andequilibrated for 5 min. Then 2 mg of dimethylsilyl bis(indenyl)hafniumdimethyl and 6 mg of [DMAH]⁺[(C₆F₅)₄B]⁺ in 5 mL of toluene were injectedusing a catalyst tube. After 15 min, the reactor was cooled to 25° C.and vented. The polymer was collected by filtration and dried in air for12 hours. Yield: 40 g.

Example 4

A 2-liter autoclave reactor was charged with toluene (1 L), propylene(150 mL), 10 g of the polyethylene macromer from Example 1 andTriisobutylaluminum (2.0 mL of 1M solution in toluene). The reactor washeated to 90° C. and equilibrated for 5 min. Then 2 mg of dimethylsilylbis(2-methyl indenyl) zirconium dichloride activated in 5 mL of tolueneand 1 mL of MAO (10 wt % in toluene) was injected using a catalyst tube.After 15 min, the reactor was cooled to 25° C. and vented. The polymerwas collected by filtration and dried in air for 12 hours. Yield: 40 g.

Example 5

A 2-liter autoclave reactor was charged with toluene (1 L), propylene(150 mL), 10 g of the polyethylene macromer from Example 2 andTriisobutylaluminum (2.0 mL of 1M solution in toluene). The reactor washeated to 50° C. and equilibrated for 5 min. Then 2 mg of dimethylsilylbis(2-methyl indenyl) zirconium dichloride activated in 5 mL of tolueneand 1 mL of MAO (10 wt % in toluene) was injected using a catalyst tube.After 15 min, the reactor was cooled to 25° C. and vented. The polymerwas collected by filtration and dried in air for 12 hours. Yield: 53 g.

Example 6

A 2-liter autoclave reactor was charged with toluene (1 L), propylene(150 mL), 5 g of the polyethylene macromer from Example 2 andTriisobutylaluminum (2.0 mL of 1M solution in toluene). The reactor washeated to 50° C. and equilibrated for 5 min. Then 2 mg of dimethylsilylbis(2-methyl indenyl) zirconium dichloride activated in 5 mL of tolueneand 1 mL of MAO (10 wt % in toluene) was injected using a catalyst tube.After 15 min, the reactor was cooled to 25° C. and vented. The polymerwas collected by filtration and dried in air for 12 hours. Yield: 51 g.

Comparative Example 7

A 2-liter reactor was charged with toluene (1 L), propylene (150 mL),and Triisobutylaluminum (2.0 mL of 1M solution in toluene). The reactorwas heated to 50° C. and equilibrated for 5 min. Then 2 mg ofdimethylsilyl bis(2-methyl indenyl) zirconium dichloride activated in 5mL of toluene and 1 mL of MAO (10 wt % in toluene) was injected using acatalyst tube. After 15 min, the reactor was cooled to 25° C. andvented. The polymer was collected by filtration and dried in air for 12hours. Yield: 63 g.

Product Characterization

Some general characterization data for the polymers made in the Examples3-6 and Comparative Example 7 are listed in Table 1. The polymer productsamples were analyzed by gel permeation chromatography using a Waters150C high temperature system equipped with a DRI Detector, ShodexAT-806MS column and operating at a system temperature of 145° C. Thesolvent used was 1,2,4-trichlorobenzene, from which polymer samplesolutions of 1.5 mg/ml concentration were prepared for injection. Thetotal solvent flow rate was 1 ml/minute and the injection size was 300microliters. After elution of the polymer samples, the resultingchromatograms were analyzed using the Waters Expert Ease program tocalculate the molecular weight distribution and one or more of M_(n),M_(w) and M_(z) averages.

The melting point of the polymer product samples was determined on a DSC2910 Differential Scanning Calorimeter (TA Instruments). The reportedmelting points were recorded at second melt with a temperature ramp of10° C./min. “Wt. % C₂” indicates the percentage of polyethylene macromer(C₂) incorporated into the polymer samples which was determined byAnalytical Composition Distribution analysis.

TABLE 1 Physical Data Summary Example Mw MWD Tm (° C.) Wt. % C₂ 3 76,2782.07 127 4 4 53,844 2.37 148 9 5 164,394 4.62 147 10 6 138,267 3.78 1493 Comp. 7 154,267 1.68 149 0

Additional analysis was conducted on the polymer produced in Example 4to determine the amount of branching and branch distribution. Since theethylene contents at various molecular weight regions can be readilydetermined by FTIR, it is possible to quantify the incorporation ofmacromer and calculate LCB distribution. Shown in FIG. 1 is the GPC-FTIRanalysis for the polymer made in Example 4. The dots indicate theethylene content measured by FTIR at different molecular weight alongthe GPC curve. Since the molecular weight (Mn) of the PE macromer is7,500, the ethylene content detected at high molecular region clearlyindicates the incorporation of macromer in the PP backbones. Moreimportantly, it is possible to calculate the statisticalLCB-distribution (also shown in FIG. 1). Assuming that all macromershave the equal probability of incorporation (all macromers are equallyspaced along the PP backbones), then, the number of long chain branchesat certain molecular weight may be calculated according to the followingequation:${\# \quad {of}\quad {LCB}\text{/}{Chain}} = \frac{\left( {{{MW}\quad {of}\quad {Polymer}},\quad {DRI}} \right)\left( {{{wt}.\quad {fraction}}\quad {of}\quad {PE}} \right)}{\left( {{Mn}{\quad \quad}{of}{\quad \quad}{Macromer}} \right)\left( {1 - {{{wt}.\quad {fraction}}\quad {of}\quad {PE}}} \right)}$

FIG. 2 shows a complex viscosity vs. shear rate curve for the polymersproduced in Example 5 and Comparative Example 7. Example 5 demonstratesa steeper curve than Comparative Example 7. A steeper curve correlatesto improved shear thinning performance as the viscosity reduces morerapidly at high shear rates. Therefore, the polymer product which wasproduced using macromers demonstrates improved processability over apolymer which was produced without the use of macromers.

While certain representative embodiments and details have been shown forthe purposes of illustrating the invention, it will be apparent to thoseskilled in the art that various changes in the process and productsdisclosed herein may be made without departing from the scope of theinvention, which is defined in the appended claims.

We claim:
 1. A branched olefin copolymer having an syndiotacticpolypropylene backbone, optionally comprising monomer units from one ormore comonomers, and sidechains derived from macromers comprising: (a)vinyl ended copolymer chains having a number average molecular weight(M_(n)) of about 1500 to 75,000, the number average molecular weightbeing determined by gel permeation chromatography (GPC) at 145° C.; and(b) a ratio of vinyl groups to total olefin groups according to theformula: (vinyl groups/olefin groups)> (comonomer molepercentage+0.1)^(a)×10_(a) ×b, wherein a=−0.24 and b=0.8; or a=−0.20 andb=0.8; or a=−0.18 and b=0.83; or a=−0.15, b=0.83; or a=−0.10 and b=0.85;wherein: 1) the total number of vinyl groups per 1000 carbon atoms ofthe sidechains is greater than or equal to 8000÷M_(n)(as measured by¹H-NMR at 125° C.); 2) the M_(w)/M_(n) of the sidechains ranges from2.083 to 5.666; and 3) the vinyl ended copolymer chains compriseethylene and at least one comonomer selected from C₃ to C₁₂ α-olefins.2. The branched olefin polymer of claim 1 wherein backbone contains 0mole percent comonomer.
 3. The branched olefin polymer of claim 1wherein the backbone further comprises one or more comonomers selectedfrom the group consisting of ethylene, C₄-C₂₀ α-olefins, geminallydisubstituted olefins, C₅-C₂₅ cyclic olefins, C₈-C₂₅ styrenic olefins,and C₃-C₈ alkyl substituted analogs of the cyclic and styrenic olefins.4. The branched olefin polymer of claim 1 where the total comonomercontent of the branched olefin copolymer is from 3 to 20 mole percent ofsaid branched olefin copolymer.
 5. The polyolefin product of claim 1where the total comonomer content of the branched olefin copolymer isfrom 5 to 17 mole percent of said branched olefin copolymer.
 6. Thebranched olefin polymer of claim 1 wherein the sidechains contain 1 to15 mole percent of comonomer.
 7. The branched olefin polymer of claim 1wherein the sidechains contain 1 to 10 mole percent of comonomer.
 8. Thebranched olefin polymer of claim 1 wherein the sidechains contain 2 to 6mole percent of comonomer.
 9. The branched olefin polymer of claim 1wherein the sidechains have an Mn above 3000 and a comonomer content of0.2 to 4.0 mole percent.
 10. The branched olefin polymer of claim 1wherein the sidechains have an Mn above 3000 and 0.2 to 4.0 mole percentof 1-octane and/or 1-butene.
 11. The branched olefin polymer of claim 1wherein the sidechains have a melt enthalpy of less than or equal to 90cal/g.
 12. The branched olefin polymer of claim 1 wherein the sidechainscomprise ethylene, at least one comonomer selected from C₃ to C₁₂α-olefins and at least one additional comonomer.
 13. The branched olefinpolymer of claim 1 wherein the sidechains comprise ethylene, at leastone comonomer selected from C₃ to C₁₂ α-olefins and at least oneadditional comonomer selected from the group consisting of C₃-C₂₀α-olefins, geminally disubstituted olefins, C₅-C₂₅ cyclic olefins,C₁-C₂₅ styrenic olefins, and C₃-C₈ alkyl substituted analogs of thecyclic and styrenic olefins.
 14. The branched olefin polymer of claim 1wherein the sidechains comprise a mixture of sidechains with differentmolecular weights and/or compositions.
 15. The branched olefin polymerof claim 1 wherein the sidechains comprise 1 to 10 mole percent of oneor more comonomers; and the backbone comprises one or more comonomersselected from the group consisting of C₃-C₂₀ α-olefins; and the totalcomonomer content of the branched olefin polymer is from 3 to 20 molepercent.
 16. The branched olefin polymer of claim 1 wherein thesidechains have an Mn of more than 3000 and from 0.2 to 4.0 mole percentof one or more of 1-octene and/or 1-butane and the backbone ishomopolypropylene.
 17. The branched olefin polymer of claim 1 whereinthe sidechains have an Mn of more than 3000 and from 0.2 to 4.0 molepercent of 1-octane and/or, 1-butene, and the backbone is copolymer ofpropylene and one or more of ethylene and/or C₄ to C₂₀ alpha-olefins.18. The branched olefin polymer of claim 1 wherein the sidechains arehave an Mn of more than 3000 and from 0.2 to 4.0 mole percent of1-octane and/or 1-butene; and the backbone is a copolymer of propyleneand one or more of ethylene and/or C₄ to C₂₀ α-olefins; and the totalcomonomer content of the branched olefin polymer is from 3 to 20 molepercent.
 19. The branched olefin polymer of claim 1 wherein thesidechains have an Mn of more than 3000 and from 0.2 to 4.0 mole percentof one or more of 1-octene and/or 1-butene; and the backbone is acopolymer of propylene and ethylene and/or one or more C₄ to C₂₀alpha-olefins; and the total comonomer content of the branched olefinpolymer is from 5 to 17 mole percent.
 20. A process to produce abranched olefin copolymer having an syndiotactic polypropylene backbone,optionally comprising monomer units from one or more comonomers, andsidechains derived from macromers comprising: a) contacting ethylene andit least one C₃ to C₁₂ olefin comonomer with a transition metal olefinpolymerization catalyst activated by an alumoxane cocatalyst, the moleratio of aluminum to transition metal is between 20:1 and 175:1, in asolution at a temperature of 30 to 150° C. and a pressure of up to 345MPa; b) obtaining a polymer product having: 1) greater than 40% chainend-group unsaturation, 2) a number average molecular weight (Mn) ofabout 1500 to 75,000, (as measured by gel permeation chromatography(GPC) at 145° C.), 3) a ratio of vinyl groups to total olefin groupsaccording to the formula: (vinyl groups/olefin groups)> (comonomer molepercentage+0.1)×10^(a) ×b, wherein a=−0.24 and b=0.8; or a=−0.20 andb=0.8; or a=−0.18 and b=0.83; or a=−0.15, b=0.83; or a=−0.10 and b=0.85,4) a total number of vinyl groups per 1000 carbon atoms greater than orequal to 8000÷Mn (as determined by ¹H-NMR at 125° C.), and 5) an Mw/Mnranging from 2.083 to 5.666; c) copolymerizing the polymer product withpropylene and, optionally, one or more copolymerizable monomers, in apolymerization reactor under suitable polypropylene polymerizationconditions using a chiral, stereorigid transition metal catalyst capableof producing syndiotactic polypropylene; and d) recovering a branchedolefin copolymer.
 21. The process of claim 20 wherein step (a) isconducted by a solution process in which said ethylene and one or morecopolymerizable monomers are contacted with a transition metal olefinpolymerization catalyst activated by an alumoxane cocatalyst, the moleratio of aluminum to transition metal is between 20:1 and 140:1.
 22. Theprocess of claim 21 wherein step (c) is conducted in a separate reactionby solution, shiny, or gas phase polymerization.
 23. The process ofclaim 22 wherein said chiral, stereorigid transition metal catalystcompound in step (c) is activated by an alumoxane cocatalyst ornon-coordinating anion precursor.
 24. The process of claim 23 whereinthe chiral, stereorigid transition metal catalyst compound in step (c)comprises one or moreDimethylsilandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂Dimethylsilandiylbis(2-methyl-4,5-benzoindenyl)ZrCl₂;Dimethylsilandiylbis(2-methyl-4,6-diisopropylindenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-phenyl-1-indenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-naphthyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(2-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4,6-trimethyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-t-butyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-4-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4-dimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(methylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(tetramethylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2,4,7-trimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-t-butyl-1-indenyl)ZrCl₂, orDimethylsilandiylbis(2,5,6-trimethyl-1-indenyl)ZrCl₂.
 25. The process ofclaim 23 wherein the chiral, stereorigid transition metal catalystcompound in step (c) comprises one or more of: dimethylsilylbis(2-methyl-indenyl)ZrCl₂, dimethylsilylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂, dimethylsilylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂, or dimethylsilylbis(indenyl)hafnium dimethyl.
 26. The process of claim 21 wherein step(c) is conducted in a separate reaction by bulk liquid propylenepolymerization.
 27. The process of claim 22 wherein step (c) isconducted in a separate reaction by bulk liquid propylenepolymerization.
 28. A process to produce a branched olefin copolymerhaving an syndiotactic polypropylene backbone, optionally comprisingmonomer units from one or more comonomers, and sidechains derived frommacromers comprising: a) contacting ethylene and, optionally with one ormore copolymerizable monomers, with a transition metal olefinpolymerization catalyst activated by an alumoxane cocatalyst, the moleratio of aluminum to transition metal is between 20:1 and 175:1, in asolution at a temperature of 30 to 150° C. and a pressure of up to 345MPa; b) obtaining a polymer product having: 1) greater than 40% chainend-group unsaturation, 2) a number average molecular weight (Mn) ofabout 1500 to 25,154, (as measured by gel permeation chromatography(GPC) at 145° C.), 3) a ratio of vinyl groups to total olefin groupsaccording to the formula: (vinyl groups/olefin groups)> (comonomer molepercentage+0.1)^(a)×10^(a) ×b, wherein a=−0.24 and b=0.8; or a=−0.20 andb=0.8; or a=−0.18 and b=0.83; or a=−0.15, b=0.83; or a=−0.10 and b=0.85,4) a total number of vinyl groups per 1000 carbon atoms greater than orequal to 8000÷Mn (as determined by ¹H-NMR at 125° C.), and 5) an Mw/Mnranging from 2.083 to 5.666; c) copolymerizing the polymer product withpropylene and, optionally, one or more copolymerizable monomers, in apolymerization reactor under suitable polypropylene polymerizationconditions using a chiral, stereorigid transition metal catalyst capableof producing syndiotactic polypropylene; and d) recovering a branchedolefin copolymer having a total comonomer content of from 0 to 20 molepercent; and a mass ratio of the syndiotactic polypropylene to thesidechains ranging from 99.9:0.1 to 50:50.
 29. The process of claim 28wherein step (a) is conducted by a solution process in which saidethylene and one or more copolymerizable monomers are contacted with atransition metal olefin polymerization catalyst activated by analumoxane cocatalyst, the mole ratio of aluminum to transition metal isbetween 20:1 and 140:1.
 30. The process of claim 29 wherein step (c) isconducted in a separate reaction by solution, slurry, or gas phasepolymerization.
 31. The process of claim 30 wherein said chiral,stereorigid transition metal catalyst compound in step (c) is activatedby an alumoxane cocatalyst or non-coordinating anion precursor.
 32. Theprocess of claim 30 wherein the chiral, stereorigid transition metalcatalyst compound in step (c) comprises one or more of:Dimethylsilandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂Dimethylsilandiylbis(2-methyl-4,5-benzoindenyl)ZrCl₂;Dimethylsilandiylbis(2-methyl-4,6-diisopropylindenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-phenyl-1-indenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-naphthyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(2-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4,6-trimethyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-t-butyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-4-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4-dimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(methylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(tetramethylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2,4,7-trimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-t-butyl-1-indenyl)ZrCl₂, orDimethylsilandiylbis(2,5,6-trimethyl-1-indenyl)ZrCl₂.
 33. The process ofclaim 30 wherein the chiral, stereorigid transition metal catalystcompound in step (c) comprises one or more of: dimethylsilylbis(2-methyl-indenyl)ZrCl₂, dimethylsilylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂, dimethylsilylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂, or dimethylsilylbis(indenyl)hafnium dimethyl.
 34. A process to produce a branched olefincopolymer having an syndiotactic polypropylene backbone, optionallycomprising monomer units from one or more comonomers, and sidechainsderived from macromers comprising: a) contacting ethylene and at leastone C₃ to C₁₂ olefin comonomer with a transition metal olefinpolymerization catalyst activated by an alumoxane cocatalyst, the moleratio of aluminum to transition metal is between 20:1 and 175:1, in asolution at a temperature of 30 to 150° C. and a pressure of up to 345MPa; b) obtaining a polymer product having: 1) greater than 40% chainend-group unsaturation, 2) a number average molecular weight (Mn) ofabout 1500 to 75,000, (as measured by gel permeation chromatography(GPC) at 145° C.), 3) a ratio of vinyl groups to total olefin groupsaccording to the formula: (vinyl groups/olefin groups)>(comonomer molepercentage+0.1)^(a)×10^(a) ×b, wherein a=−0.24 and b=0.8; or a=−0.20 andb=0.8; or a=−0.18 and b=0.83; or a=−0.15, b=0.83; or a=−0.10 and b=0.85,4) a total number of vinyl groups per 1000 carbon atoms greater than orequal to 8000÷Mn (as determined by ¹H-NMR at 125° C.), and 5) an Mw/Mnranging from 2.083 to 5.666; c) copolymerizing the polymer product withpropylene and, optionally, one or more copolymerizable monomers, in apolymerization reactor under suitable polypropylene polymerizationconditions using a chiral, stereorigid transition metal catalyst capableof producing syndiotactic polypropylene; and d) recovering a branchedolefin copolymer.
 35. The process of claim 34 wherein step (a) isconducted by a solution process in which said ethylene and one or morecopolymerizable monomers are contacted with a transition metal olefinpolymerization catalyst activated by an alumoxane cocatalyst, the moleratio of aluminum to transition metal is between 20:1 and 140:1.
 36. Theprocess of claim 35 wherein step (c) is conducted in a separate reactionby solution, slurry, or gas phase polymerization.
 37. The process ofclaim 36 wherein said chiral, stereorigid transition metal catalystcompound in step (c) is activated by an alumoxane cocatalyst ornon-coordinating anion precursor.
 38. The process of claim 37 whereinthe chiral, stereorigid transition metal catalyst compound in step (c)comprises one or more of:Dimethylsilandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂Dimethylsilandiylbis(2-methyl-4,5-benzoindenyl)ZrCl₂;Dimethylsilandiylbis(2-methyl-4,6-diisopropylindenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-phenyl-1-indenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-naphthyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(2-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4,6-trimethyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-t-butyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-4-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4-dimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(methylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(tetramethylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2,4,7-trimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-t-butyl-1-indenyl)ZrCl₂, orDimethylsilandiylbis(2,5,6-trimethyl-1-indenyl)ZrCl₂.
 39. A branchedolefin polymer having an syndiotactic polypropylene backbone, optionallycomprising monomer units from one or more comonomers, and sidechainsderived from macromers comprising: (a) vinyl ended ethylene homopolymeror ethylene copolymer chains having a number average molecular weight(Mn) of about 1500 to 25,154, the number average molecular weight beingdetermined by gel permeation chromatography (QPC) at 145° C.; and (b) aratio of vinyl groups to total olefin groups according to the formula:(vinyl groups/olefin groups)> (comonomer mole percentage+0.1)^(a)×10^(a)×b, wherein a=−0.24 and b=0.8; or a=−0.20 and b=0.8; or a=−0.18 andb=0.83; or a=−0.15, b=0.83; or a=−0.10 and b=0.85; wherein: 1) the totalnumber of vinyl groups per 1000 carbon atoms of the sidechains isgreater than or equal to 8000+Mn (as determined by ¹H-NMR at 125° C.);2) the Mw/Mn of the side chains ranges from 2.083 to 5.666; 3) the totalcomonomer content of the branched olefin copolymer is from 0 to 20 molepercent; and 4) the mass ratio of the syndiotactic polypropylene to thesidechains ranges from 99.9:0.1 to 50:50.
 40. The branched olefinpolymer of claim 39 wherein the backbone contains 0 mole percentcomonomer.
 41. The branched olefin polymer of claim 39 wherein thebackbone further comprises one or more comonomers selected from thegroup consisting of ethylene, C₄-C₂₀ α-olefins, geminally disubstitutedolefins, C₅-C₂₅ cyclic olefins, and C₃-C₈ alkyl substituted analogs ofthe cyclic olefins.
 42. The branched olefin polymer of claim 39 whereinthe backbone further comprises one or more comonomers selected from thegroup consisting of ethylene, C₄-C₂₀ α-olefins, geminally disubstitutedmonomers, C₅-C₂₅ cyclic olefins, C₅-C₂₅ styrenic olefins, and lowercarbon number (C₃-C₈) alkyl substituted analogs of the cyclic andstyrenic olefins.
 43. The polyolefin product of claim 39 where the totalcomonomer content of the branched olefin copolymer is from 5 to 17 molepercent of said branched olefin copolymer.
 44. The branched olefincopolymer of claim 39 wherein the mass ratio of the backbone to thesidechains ranges from 95:5 to 50:50.
 45. The branched olefin polymer ofclaim 39 wherein the sidechains contain 0 mole percent of comonomer. 46.The branched olefin polymer of claim 39 wherein the sidechains contain 0to 15 mole percent of comonomer.
 47. The branched olefin polymer ofclaim 39 wherein the sidechains contain 1 to 10 mole percent ofcomonomer.
 48. The branched olefin polymer of claim 39 wherein thesidechains contain 2 to 6 mole percent of comonomer.
 49. The branchedolefin polymer of claim 39 wherein the sidechains further comprise oneor more comonomers selected from the group consisting of C₃-C₂₀α-olefins, geminally disubstituted olefins, C₅-C₂₅ cyclic olefins,C₈-C₂₅ styrenic olefins, and C₃-C₈ alkyl substituted analogs of thecyclic and styrenic olefins.
 50. The branched olefin polymer of claim 39wherein the sidechain has an Mn above 3000 and a comonomer content of0.2 to 4.0 mole percent.
 51. The branched olefin polymer of claim 39wherein the sidechain has an Mn above 3000 and 0.2 to 4.0 mole percentof a comonomer selected from the group consisting of 1-octene, 1-butene,norbornene and alkyl substituted norbornene.
 52. The branched olefinpolymer of claim 39 wherein the sidechain has a melt enthalpy of lessthan or equal to 90 cal/g.
 53. The branched olefin polymer of claim 39wherein the sidechains are have an Mn of more than 3000 and from 0.2 to4.0 mole percent of one or more of 1-octene, norbornene, and 1-butene.54. The branched olefin polymer of claim 39 wherein the sidechainscomprise ethylene, at least one comonomer selected from C₃ to C₁₂α-olefins and at least one additional comonomer.
 55. The branched olefinpolymer of claim 39 wherein the sidechains comprise ethylene, at leastone comonomer selected from C₃ to C₁₂ α-olefins and at least oneadditional comonomer selected from the group consisting of C₃-C₂₀αolefins, geminally disubstituted olefins, C₅-C₂₅ cyclic olefins, C₈-C₂₅styrenic olefins, and C₃-C₈ alkyl substituted analogs of the cyclic andstyrenic olefins.
 56. The branched olefin polymer of claim 39 where thetotal comonomer content of the branched olefin copolymer is from 3 to 20mole percent of said branched olefin copolymer.
 57. The polyolefinproduct of claim 39 where the total comonomer content of the branchedolefin copolymer is from 5 to 17 mole percent of said branched olefincopolymer.
 58. The branched olefin polymer of claim 39 wherein thesidechains comprise one or more comonomers selected from the groupconsisting of C₃-C₂₀ α-olefins, geminally disubstituted monomers, C₅-C₂₅cyclic olefins, C₈-C₂₅ styrenic olefins, and C₃-C₈ alkyl substitutedanalogs of the cyclic and styrenic olefins; and, the backbone comprisesone or more comonomers selected from the group consisting of ethylene,C₄-C₂₀ α-olefins, geminally disubstituted olefins, C₅-C₂₅ cyclicolefins, C₈-C₂₅ styrenic olefins, and C₃-C₈ alkyl substituted analogs ofthe cyclic and styrenic olefins.
 59. The branched olefin polymer ofclaim 39 wherein the sidechains comprise 1 to 10 mole percent of one ormore comonomers selected from the group consisting of C₃-C₂₀ α-olefins,geminally disubstituted olefins, C₅-C₂₅ cyclic olefins, C₈-C₂₅ styrenicolefins, and C₃-C₈ alkyl substituted analogs of the cyclic and styrenicolefins; and the backbone comprises one or more comonomers selected fromthe group consisting of ethylene, C₄-C₂₀ α-olefins, geminallydisubstituted olefins, C₅-C₂₅ cyclic olefins, C₈-C₂₅ styrenic olefins,and C₃-C₈ alkyl substituted analogs of the cyclic and styrenic olefins;and the total comonomer content of the branched olefin polymer is from 3to 20 mole percent.
 60. The branched olefin polymer of claim 39 whereinthe sidechains comprise 1 to 10 mole percent of one or more comonomersselected from the group consisting of C₃-C₂₀ α-olefins; and the backbonecomprises one or more comonomers selected from the group consisting ofethylene and C₄-C₂₀ α-olefins; and the total comonomer content of thebranched olefin polymer is from 3 to 20 mole percent.
 61. The branchedolefin polymer of claim 39 wherein the sidechains are homopolyethyleneand the backbone is homopolypropylene.
 62. The branched olefin polymerof claim 39 wherein the sidechains have an Mn of more than 3000 and from0.2 to 4.0 mole percent of one or more of 1-octene, norbornene, and1-butene; and the backbone is a copolymer of propylene and one or moreof ethylene and/or C₄ to C₂₀ α-olefins; and the total comonomer contentof the branched olefin polymer is from 5 to 17 mole percent.
 63. Thebranched olefin polymer of claim 39 wherein the sidechains have an Mn ofmore than 3000 and from 0.2 to 4.0 mole percent of one or more of1-octene, 1-butene, norbornene, or alkyl-substituted norbornene, and thebackbone is homopolypropylene.
 64. The branched olefin polymer of claim39 wherein the sidechains have an Mn of more than 3000 and from 0.2 to4.0 mole percent of 1-octene and/or 1-butene; and the backbone is acopolymer of propylene and one or more of ethylene and/or C₄ to C₂₀α-olefins; and the total comonomer content of the branched olefinpolymer is from 3 to 20 mole percent.
 65. The branched olefin polymer ofclaim 39 wherein the sidechains have an Mn of more than 3000 and from0.2 to 4.0 mole percent of one or more of 1-octene, norbornene or1-butene, and the backbone is homopolypropylene.
 66. The branched olefinpolymer of claim 39 wherein the sidechains have an Mn of more than 3000and from 0.2 to 4.0 mole percent of one or more of 1-octene, 1-butene,norbornene, or alkyl-substituted norbornene and the backbone iscopolymer of propylene and one or more of ethylene and/or C₄ to C₂₀α-olefins.
 67. A process to produce a branched olefin copolymer having asyndiotactic polypropylene backbone, optionally comprising monomer unitsfrom one or more comonomers, and sidechains derived from macromerscomprising: a) contacting ethylene and, optionally with one or morecopolymerizable monomers, with a transition metal olefin polymerizationcatalyst activated by an alumoxane cocatalyst, the mole ratio ofaluminum to transition metal is between 20:1 and 175:1, in a solution ata temperature of 30 to 150° C. and a pressure of up to 345 MPa; b)obtaining a polymer product having: 1) greater than 40% chain end-groupunsaturation, 2) a number average molecular weight (Mn) of about 1500 to25,154, (as measured by gel permeation chromatography (GPC) at 145° C.),3) a ratio of vinyl groups to total olefin groups according to theformula: (vinyl groups/olefin groups)>(comonomer molepercentage+0.1)^(a)×10^(a) ×b, wherein a=−0.24 and b=0.8; or a=−0.20 andb=0.8; or a=−0.18 and b=0.83; or a=−0.15, b=0.83; or a=−0.10 and b=0.85,4) a total number of vinyl groups per 1000 carbon atoms greater than orequal to 8000÷Mn (as determined by ¹H-NMR at 125° C.), and 5) an Mw/Mnranging from 2.083 to 5.666; c) copolymerizing the polymer product withpropylene and, optionally, one or more copolymerizable monomers, in apolymerization reactor under suitable polypropylene polymerizationconditions using a chiral, stereorigid transition metal catalyst capableof producing syndiotactic polypropylene; and d) recovering a branchedolefin copolymer having a total comonomer content of from 0 to 20 molepercent; and a mass ratio of the syndiotactic polypropylene to thesidechains ranging from 99.9:0.1 to 50:50.
 68. The process of claim 67wherein step (a) is conducted by a solution process in which saidethylene and one or more copolymerizable monomers are contacted with atransition metal olefin polymerization catalyst activated by analumoxane cocatalyst, the mole ratio of aluminum to transition metal isbetween 20:1 and 140:1.
 69. The process of claim 68 wherein step (c) isconducted in a separate reaction by solution, slurry, or gas phasepolymerization.
 70. The process of claim 69 wherein said chiral,stereorigid transition metal catalyst compound in step (c) is activatedby an alumoxane cocatalyst or non-coordinating anion precursor.
 71. Theprocess of claim 69 wherein the chiral, stereorigid transition metalcatalyst compound in step (c) comprises one or more of:Dimethylsilandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂Dimethylsilandiylbis(2-methyl-4,5-benzoindenyl)ZrCl₂;Dimethylsilandiylbis(2-methyl-4,6-diisopropylindenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-phenyl-1-indenyl)ZrCl₂;Dimethylsilandiylbis(2-ethyl-4-naphthyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-(2-naphthyl)-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4,6-trimethyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,6-diisopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-t-butyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4-isopropyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-4-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2,4-dimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(methylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-4,5-(tetramethylbenzo)-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-α-acenaphth-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-4,5-benzo-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2,4,7-trimethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Ethandiylbis(2-methyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-1-indenyl)ZrCl₂,1,2-Butandiylbis(2-methyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-ethyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Phenyl(Methyl)silandiylbis(2-methyl-5-isobutyl-1-indenyl)ZrCl₂,Dimethylsilandiylbis(2-methyl-5-t-butyl-1-indenyl)ZrCl₂, orDimethylsilandiylbis(2,5,6-trimethyl-1-indenyl)ZrCl₂.
 72. The process ofclaim 69 wherein the chiral, stereorigid transition metal catalystcompound in step (c) comprises one or more of: dimethylsilylbis(2-methyl-indenyl)ZrCl₂, dimethylsilylbis(2-methyl-4-phenyl-1-indenyl)ZrCl₂, dimethylsilylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂, or dimethylsilylbis(indenyl)hafnium dimethyl.
 73. The process of claim 37 wherein thechiral, stereorigid transition metal catalyst compound in step (c)comprises one or more of: dimethylsilyl bis(2-methyl-indenyl)ZrCl₂,dimethylsilyl bis(2-methyl-4-phenyl-1-indenyl)ZrCl₂, dimethylsilylbis(2-methyl-4-(1-naphthyl)-1-indenyl)ZrCl₂, or dimethylsilylbis(indenyl)hafnium dimethyl.